Syngas Fermentation Process and Medium

ABSTRACT

A process for fermenting syngas and a fermentation medium provides high ethanol productivity while removing medium components that were previously thought to be essential. The process is effective for providing a specific STY of at least about 1 g ethanol/(L·day·gram cells). In this aspect, the fermentation medium has a weight ratio of NH 4   +  to B of about 625:1 or more, or a weight ratio of NH 4   +  to Mn of about 4050:1 or more, or a weight ratio of NH 4   +  to Mo of about 2500:1 or more, or a ratio of NH 4   +  to Cu of about 4050:1 or more; or the fermentation medium has a weight ratio of P to B of about 30:1 or more, or a weight ratio of P to Mn of about 190:1 or more, or a weight ratio of P to Mo of about 120:1 or more, or a weight ratio of Mn to Cu of about 190:1 or more; or the fermentation medium has a weight ratio of K to B of about 35:1 or more, or a weight ratio of K to Mn of about 245:1 or more, or a weight ratio of K to Mo of about 150:1 or more, or a weight ratio of K to Cu of about 245:1 or more.

This application claims the benefit of U.S. Provisional Application Nos.61/650,098, 61/650,093, 61/650,077, 61/650,084 all filed on May 22, 2012and U.S. Provisional Application No. 61/726,225 filed on Nov. 14, 2012,all of which are incorporated in their entirety herein by reference.

Processes and mediums are provided for fermentation of syngas. Morespecifically, processes and mediums are provided that provide a highlevel of ethanol productivity even after removing or reducingconcentrations of components that were previously considered to beessential or required at certain concentration levels.

BACKGROUND

Fermentations take place in defined liquid mediums. These mediums willtypically include various macro- and micro-nutrient sources that areimportant in improving fermentation performance. Mediums used inconnection with less common substrates, such as gaseous substrates,require well defined mediums to optimize performance. Anaerobicfermentations also require well defined mediums.

Anaerobic microorganisms can produce ethanol from carbon monoxide (CO)through fermentation of gaseous substrates. Fermentations usinganaerobic microorganisms from the genus Clostridium produce ethanol andother useful products. For example, U.S. Pat. No. 5,173,429 describesClostridium ljungdahlii ATCC No. 49587, an anaerobic microorganism thatproduces ethanol and acetate from synthesis gas. U.S. Pat. No. 5,807,722describes a method and apparatus for converting waste gases into organicacids and alcohols using Clostridium ljungdahlii ATCC No. 55380. U.S.Pat. No. 6,136,577 describes a method and apparatus for converting wastegases into ethanol using Clostridium ljungdahlii ATCC No. 55988 and55989.

U.S. Pat. No. 7,285,402 describes mediums known for use in anaerobicfermentation of gaseous substrates to produce ethanol. Various componentand component concentrations in the medium are effective for providinghigh levels of ethanol productivity. Eliminating certain components andreducing required concentrations levels of other components whilemaintaining ethanol productivity may provide significant cost savings,especially at a commercial scale fermentation.

SUMMARY

A process for fermenting syngas and a fermentation medium provides highethanol productivity while removing medium components that werepreviously thought to be essential. Removal of certain medium componentsand reducing concentrations of other medium components providessignificant operational cost savings at a commercial scale.

In one aspect, a fermentation process includes fermenting syngas in afermentation medium. The process is effective for providing a specificSTY of at least about 1 g ethanol/(L·day·gram cells). In this aspect,the fermentation medium has less than about 1.04 ppm boron, less thanabout 0.16 ppm manganese, less than about 0.26 ppm molybdenum, or lessthan about 0.16 ppm copper.

In another aspect, a fermentation medium includes at least about 112 mgof nitrogen per gram of cells produced, at least about 10.5 mg ofphosphorous per gram of cells produced, or at least about 26 mg ofpotassium per gram of cells produced. In another aspect, thefermentation medium has less than about 1.04 ppm boron, less than about0.16 ppm manganese, less than about 0.26 ppm molybdenum, or less thanabout 0.16 ppm copper.

In another aspect, a fermentation process includes fermenting syngas ina fermentation medium. The process effective for providing a specificSTY of at least about 1 gram of ethanol/(L·day·gram cells). Thefermentation medium has a weight ratio of NH₄₊ to B of about 625:1 ormore, or a weight ratio of NH₄ ⁺ to Mn of about 4050:1 or more, or aweight ratio of NH₄ ⁺ to Mo of about 2500:1 or more, or a ratio of NH₄ ⁺to Cu of about 4050:1 or more; or the fermentation medium has a weightratio of P to B of about 30:1 or more, or a weight ratio of P to Mn ofabout 190:1 or more, or a weight ratio of P to Mo of about 120:1 ormore, or a weight ratio of Mn to Cu of about 190:1 or more; or thefermentation medium has a weight ratio of K to B of about 35:1 or more,or a weight ratio of K to Mn of about 245:1 or more, or a weight ratioof K to Mo of about 150:1 or more, or a weight ratio of K to Cu of about245:1 or more.

DETAILED DESCRIPTION

The following description is not to be taken in a limiting sense, but ismade merely for the purpose of describing the general principles ofexemplary aspects. The scope of the invention should be determined withreference to the claims.

A process and medium composition are provided that surprisingly andunexpectedly provides a high level of ethanol productivity even afterremoving or reducing concentrations of one or more components that werepreviously thought to be essential or required at certain concentrationlevels. In this aspect, the medium may have reduced concentration levelsof one or more nutrients that include B, Mn, Mo, and Cu. Nutrientconcentrations in the medium may be as follows:

B: less than about 1.04 ppm B, in another aspect, less than about 1.0ppm B, in another aspect, less than about 0.75 ppm B, in another aspect,less than about 0.5 ppm B, and in another aspect, less than about 0.025ppm B;

Mn: less than about 0.16 ppm Mn, in another aspect, less than about 0.15ppm Mn, in another aspect, less than about 0.10 ppm Mn, in anotheraspect, less than about 0.05 ppm Mn, and in another aspect, less thanabout 0.0025 ppm Mn;

Mo: less than about 0.26 ppm Mo, in another aspect, less than about 0.25ppm Mo, in another aspect, less than about 0.20 ppm Mo, in anotheraspect, less than about 0.10 ppm Mo, and in another aspect, less thanabout 0.001 ppm Mo; or

Cu: less than about 0.16 ppm Cu, in another aspect, less than about 0.15ppm Cu, in another aspect, less than about 0.10 ppm B, in anotheraspect, less than about 0.05 ppm B, and in another aspect, less thanabout 0.01 ppm B.

In another aspect, weight ratios may be as follows:

NH₄ ⁺ to B: about 625:1 or more, in another aspect, about 650:1 or more,in another aspect, about 675:1 or more, in another aspect, about 700:1or more, in another aspect, about 750:1 or more, and in another aspect,about 800:1 or more; or

NH₄ ⁺ to Mn: about 4050:1 or more, in another aspect, about 4100:1 ormore, in another aspect, about 4200:1 or more, in another aspect, about4300:1 or more, in another aspect, about 4400:1 or more, and in anotheraspect, about 4500:1 or more; or

NH₄ ⁺ to Mo: about 2500:1 or more, in another aspect, about 2600:1 ormore, in another aspect, about 2700:1 or more, in another aspect, about2800:1 or more, in another aspect, about 2900:1 or more, and in anotheraspect, about 3000:1 or more; or

NH₄ ⁺ to Cu: about 4050:1 or more; in another aspect, about 4100:1 ormore, in another aspect, about 4200:1 or more, in another aspect, about4300:1 or more, in another aspect, about 4400:1 or more, and in anotheraspect, about 4500:1 or more; or

P to B: about 30:1 or more, in another aspect, about 35:1 or more, inanother aspect, about 40:1 or more, in another aspect, about 45:1 ormore, in another aspect, about 50:1 or more, and in another aspect,about 100:1 or more; or

P to Mn: about 190:1 or more, in another aspect, about 200:1 or more, inanother aspect, about 225:1 or more, in another aspect, about 250:1 ormore, in another aspect, about 275:1 or more, and in another aspect,about 300:1 or more; or

P to Mo: about 120:1 or more, in another aspect, about 130:1 or more, inanother aspect, about 140:1 or more, in another aspect, about 150:1 ormore, in another aspect, about 175:1 or more, and in another aspect,about 200:1 or more; or

P to Cu: about 190:1 or more; in another aspect, about 200:1 or more, inanother aspect, about 225:1 or more, in another aspect, about 250:1 ormore, in another aspect, about 275:1 or more, and in another aspect,about 300:1 or more; or

K to B: about 35:1 or more, in another aspect, about 40:1 or more, inanother aspect, about 45:1 or more, in another aspect, about 50:1 ormore, in another aspect, about 75:1 or more, and in another aspect,about 100:1 or more; or

K to Mn: about 245:1 or more, in another aspect, about 250:1 or more, inanother aspect, about 260:1 or more, in another aspect, about 270:1 ormore, in another aspect, about 280:1 or more, and in another aspect,about 300:1 or more; or

K to Mo: about 150:1 or more, in another aspect, about 250:1 or more, inanother aspect, about 260:1 or more, in another aspect, about 270:1 ormore, in another aspect, about 280:1 or more, and in another aspect,about 300:1 or more; or

K to Cu: about 245:1 or more, in another aspect, about 250:1 or more, inanother aspect, about 260:1 or more, in another aspect, about 270:1 ormore, in another aspect, about 280:1 or more, and in another aspect,about 300:1 or more.

DEFINITIONS

Unless otherwise defined, the following terms as used throughout thisspecification for the present disclosure are defined as follows and caninclude either the singular or plural forms of definitions belowdefined:

The term “about” modifying any amount refers to the variation in thatamount encountered in real world conditions, e.g., in the lab, pilotplant, or production facility. For example, an amount of an ingredientor measurement employed in a mixture or quantity when modified by“about” includes the variation and degree of care typically employed inmeasuring in an experimental condition in production plant or lab. Forexample, the amount of a component of a product when modified by “about”includes the variation between batches in a multiple experiments in theplant or lab and the variation inherent in the analytical method.Whether or not modified by “about,” the amounts include equivalents tothose amounts. Any quantity stated herein and modified by “about” canalso be employed in the present disclosure as the amount not modified by“about”.

The term “syngas” or “synthesis gas” means synthesis gas which is thename given to a gas mixture that contains varying amounts of carbonmonoxide and hydrogen. Examples of production methods include steamreforming of natural gas or hydrocarbons to produce hydrogen, thegasification of coal and in some types of waste-to-energy gasificationfacilities. The name comes from their use as intermediates in creatingsynthetic natural gas (SNG) and for producing ammonia or methanol.Syngas is combustible and is often used as a fuel source or as anintermediate for the production of other chemicals.

The terms “fermentation”, fermentation process” or “fermentationreaction” and the like are intended to encompass both the growth phaseand product biosynthesis phase of the process. In one aspect,fermentation refers to conversion of CO to alcohol.

The term “cell density” means mass of microorganism cells per unitvolume of fermentation broth, for example, grams/liter. In this aspect,the process and mediums are effective for providing a cell density of atleast about 1.0 g/L. Cell density may be from about 1 to about 25 g/L,in another aspect, about 1 to about 20 g/L, in another aspect, about 1to about 10 g/L, in another aspect, about 2 to about 8 g/L, in anotheraspect, about 3 to about 6 g/L, and in another aspect, about 4 to about5 g/L.

The term “cell recycle” refers to separation of microbial cells from afermentation broth and returning all or part of those separatedmicrobial cells back to the fermenter. Generally, a filtration device isused to accomplish separations.

Medium Composition

The processes and mediums described herein are effective for providing ahigh level of productivity. In this aspect, the process is effective forproviding a specific STY (specific space time yield expressed as gethanol/(L·day·gram cells) of at least about 1, in another aspect, about1 to about 10, in another aspect, about 2 to about 8, in another aspect,about 3 to about 7, and in another aspect, about 4 to about 6.

In a related aspect, productivity may be expressed as STY (space timeyield expressed as g ethanol/(L·day). In this aspect, the process iseffective for providing a STY (space time yield) of at least about 10 gethanol/(L·day). Possible STY values include about 10 g ethanol/(L·day)to about 200 g ethanol/(L·day), in another aspect, about 10 gethanol/(L·day) to about 160 g ethanol/(L·day), in another aspect, about10 g ethanol/(L·day) to about 120 g ethanol/(L·day), in another aspect,about 10 g ethanol/(L·day) to about 80 g ethanol/(L·day), in anotheraspect, about 20 g ethanol/(L·day) to about 140 g ethanol/(L·day), inanother aspect, about 20 g ethanol/(L·day) to about 100 gethanol/(L·day), in another aspect, about 40 g ethanol/(L·day) to about140 g ethanol/(L·day), and in another aspect, about 40 g ethanol/(L·day)to about 100 g ethanol/(L·day).

In another aspect, the process and mediums are effective for providing aCO conversion of at least about 5% to about 99%, in another aspect,about 10% to about 90%, in another aspect, about 20% to about 80%, inanother aspect, about 30% to about 70%, and in another aspect, about 40%to about 90%.

In one aspect, the medium includes at least one or more of a nitrogensource, at least one or more phosphorous source and at least one or moreof a potassium source. The medium may include any one of the three, anycombination of the three, and in an important aspect, includes allthree. A nitrogen source may include a nitrogen source selected from thegroup consisting of ammonium chloride, ammonium phosphate, ammoniumsulfate, ammonium nitrate, and mixtures thereof. A phosphorous sourcemay include a phosphorous source selected from the group consisting ofphosphoric acid, ammonium phosphate, potassium phosphate, and mixturesthereof. A potassium source may include a potassium source selected fromthe group consisting of potassium chloride, potassium phosphate,potassium nitrate, potassium sulfate, and mixtures thereof.

In one aspect, the medium includes one or more of iron, tungsten,nickel, cobalt, magnesium, sulfur and thiamine. The medium may includeany one of these components, any combination, and in an importantaspect, includes all of these components. An iron may include an ironsource selected from the group consisting of ferrous chloride, ferroussulfate, and mixtures thereof. A tungsten source may include a tungstensource selected from the group consisting of sodium tungstate, calciumtungstate, potassium tungstate, and mixtures thereof. A nickel sourcemay include a nickel source selected from the group consisting of nickelchloride, nickel sulfate, nickel nitrate, and mixtures thereof. A cobaltsource may include a cobalt source selected from the group consisting ofcobalt chloride, cobalt fluoride, cobalt bromide, cobalt iodide andmixtures thereof. A magnesium source may include a magnesium sourceselected from the group consisting of magnesium chloride, magnesiumsulfate, magnesium phosphate, and mixtures thereof. A sulfur source mayinclude cysteine, sodium sulfide, and mixtures thereof.

Concentrations of various components are as follows:

Concentration Range Preferred Range (expressed as mg or μg (expressed asmg or μg Component nutrient per gram of cells) nutrient per gram ofcells) nitrogen (N) 112-160 mg 140-150 mg phosphorus (P) 10.5-15 mg12-13 mg potassium (K) 26-36 mg 28-33 mg iron (Fe) 2.7-5 mg 3.0-4.0 mgtungsten (W) 10-30 μg 15-25 μg Nickel (Ni) 34-40 μg 35-37 μg Cobalt (Co)9-30 μg 15-20 μg Magnesium 4.5-10 mg 5-7 mg (Mg) Sulfur (S) 11-20 mg12-16 mg Thiamine 6.5-20 μg 7-12 μg

Process operation maintains a pH in a range of about 4.2 to about 4.8.The medium includes less than about 0.01 g/L yeast extract and less thanabout 0.01 g/L carbohydrates.

Syngas

Syngas may be provided from any know source. In one aspect, syngas maybe sourced from gasification of carbonaceous materials. Gasificationinvolves partial combustion of biomass in a restricted supply of oxygen.The resultant gas mainly includes CO and H₂. In this aspect, syngas willcontain at least about 10 mole % CO, in one aspect, at least about 20mole %, in one aspect, about 10 to about 100 mole %, in another aspect,about 20 to about 100 mole % CO, in another aspect, about 30 to about 90mole % CO, in another aspect, about 40 to about 80 mole % CO, and inanother aspect, about 50 to about 70 mole % CO. The syngas will have aCO/CO₂ ratio of at least about 0.75, in another aspect, at least about1.0, and in another aspect, at least about 1.5. Some examples ofsuitable gasification methods and apparatus are provided in U.S. Ser.Nos. 13/427,144, 13/427,193 and 13/427,247, all of which were filed onMar. 22, 2012, and all of which are incorporated herein by reference.

In another aspect, syngas utilized for propagating acetogenic bacteriamay be substantially CO. As used herein, “substantially CO” means atleast about 50 mole % CO, in another aspect, at least about 60 mole %CO, in another aspect, at least about 70 mole % CO, in another aspect,at least about 80 mole % CO, and in another aspect, at least about 90mole % CO.

Bioreactor Operation

In accordance with one aspect, the fermentation process is started byaddition of medium to the reactor vessel. The medium is sterilized toremove undesirable microorganisms and the reactor is inoculated with thedesired microorganisms. In one aspect, the microorganisms utilizedinclude acetogenic bacteria. Examples of useful acetogenic bacteriainclude those of the genus Clostridium, such as strains of Clostridiumljungdahlii, including those described in WO 2000/68407, EP 117309, U.S.Pat. Nos. 5,173,429, 5,593,886 and 6,368,819, WO 1998/00558 and WO2002/08438, strains of Clostridium autoethanogenum (DSM 10061 and DSM19630 of DSMZ, Germany) including those described in WO 2007/117157 andWO 2009/151342 and Clostridium ragsdalei (P11, ATCC BAA-622) andAlkalibaculum bacchi (CP11, ATCC BAA-1772) including those describedrespectively in U.S. Pat. No. 7,704,723 and “Biofuels and Bioproductsfrom Biomass-Generated Synthesis Gas”, Hasan Atiyeh, presented inOklahoma EPSCoR Annual State Conference, Apr. 29, 2010 and Clostridiumcarboxidivorans (ATCC PTA-7827) described in U.S. Patent Application No.2007/0276447. Other suitable microorganisms includes those of the genusMoorella, including Moorella sp. HUC22-1, and those of the genusCarboxydothermus. Each of these references is incorporated herein byreference. Mixed cultures of two or more microorganisms may be used.

Some examples of useful bacteria include Acetogenium kivui,Acetoanaerobium noterae, Acetobacterium woodii, Alkalibaculum bacchiCP11 (ATCC BAA-1772), Blautia producta, Butyribacteriummethylotrophicum, Caldanaerobacter subterraneous, Caldanaerobactersubterraneous pacificus, Carboxydothermus hydrogenoformans, Clostridiumaceticum, Clostridium acetobutylicum, Clostridium acetobutylicum P262(DSM 19630 of DSMZ Germany), Clostridium autoethanogenum (DSM 19630 ofDSMZ Germany), Clostridium autoethanogenum (DSM 10061 of DSMZ Germany),Clostridium autoethanogenum (DSM 23693 of DSMZ Germany), Clostridiumautoethanogenum (DSM 24138 of DSMZ Germany), Clostridium carboxidivoransP7 (ATCC PTA-7827), Clostridium coskatii (ATCC PTA-10522), Clostridiumdrakei, Clostridium ljungdahlii PETC (ATCC 49587), Clostridiumljungdahlii ERI2 (ATCC 55380), Clostridium ljungdahlii C-01 (ATCC55988), Clostridium ljungdahlii O-52 (ATCC 55889), Clostridium magnum,Clostridium pasteurianum (DSM 525 of DSMZ Germany), Clostridium ragsdaliP11 (ATCC BAA-622), Clostridium scatologenes, Clostridiumthermoaceticum, Clostridium ultunense, Desulfotomaculum kuznetsovii,Eubacterium limosum, Geobacter sulfurreducens, Methanosarcinaacetivorans, Methanosarcina barkeri, Morrella thermoacetica, Morrellathermoautotrophica, Oxobacter pfennigii, Peptostreptococcus productus,Ruminococcus productus, Thermoanaerobacter kivui, and mixtures thereof.

Upon inoculation, an initial feed gas supply rate is establishedeffective for supplying the initial population of microorganisms.Effluent gas is analyzed to determine the content of the effluent gas.Results of gas analysis are used to control feed gas rates. Uponreaching desired levels, liquid phase and cellular material is withdrawnfrom the reactor and replenished with medium. In this aspect, thebioreactor is operated to maintain a cell density of at least about 2grams/liter, and in another aspect, about 2 to about 50 grams/liter, invarious other aspects, about 5 to about 40 grams/liter, about 5 to about30 grams/liter, about 5 to about 20 grams/liter, about 5 to about 15grams/liter, about 10 to about 40 grams/liter, about 10 to about 30grams/liter, about 10 to about 20 grams/liter, and about 10 to about 15grams/liter. Cell density may be controlled through a recycle filter. Afurther description of bioreactor operation is set forth in U.S.Provisional Application Nos. 61/571,564, filed Jun. 30, 2011, U.S.Provisional Application No. 61/571,565, filed Jun. 30, 2011, and in U.S.Provisional Application No. 61/573,845, filed Sep. 13, 2011, all ofwhich are incorporated herein by reference.

EXAMPLES Example 1 Fermentation with Boron, Copper and ManganeseLimitations

Experiments were conducted in a bioreactor (New Brunswick BioFlo I orIIc) operated as a straight through CSTR, with no permeate purge.Bioreactor operating conditions were as follows:

Culture type was Clostridium ljungdahlii C01.

Culture temperature was kept at 38-39° C.

Agitation was 850 rpm on an analog readout.

The unroused culture volume was ˜1600-1650 ml.

The culture pH set point was 4.5. A solution of 7.7% NaHCO₃ was used forpH control.

Feed gas was a synthetic blend of 15% H₂, 45% N₂, 30% CO and 10% CO₂ fedto the culture at a rate of 282 ml/min.

Medium was fed into the reactor at ˜0.88 ml/min, or ˜1300 ml/day.

Liquid and cell retention times were approximately 29-31 hours.

The starting medium used was as described below.

Component/ Ion Added As Conc in Med (ppm) NH₄ ⁺ NH₄Cl/(NH₄)₂HPO₄ 838 FeFeCl₂•4H₂O 16.8 Ni NiCl₂•6H₂O 0.1975 Co CoCl₂•6H₂O 0.991 Se Na₂SeO₃0.0913 Zn ZnSO₄•7H₂O 0.455 Mo Na₂MoO₄•2H₂O 0.238 Mn MnCl₂•4H₂O 0.167 BH₃BO₃ 1.05 Cu CuCl₂•2H₂O 0.149 W Na₂WO₄•2H₂O 1.12 K KCl 78.6 MgMgCl₂•6H₂O 59.8 Na NaCl 78.7* Ca CaCl₂•2H₂O 54.5** Cysteine HCl CysteineHCl 250 P H₃PO₄/(NH₄)₂HPO₄ 279 *Na⁺ concentration is from NaCl only. Itdoes not include Na⁺ from the other components such as Na₂WO₄•2H₂O.**Ca⁺² concentration does not include calcium from pantothenic acid,calcium salt as other sources provide only trace or insignificantamounts of calcium.

The bioreactor was operated until the culture obtained a highproductivity steady state. High productivity steady state was defined as˜2.5-3 g/L cell density, an ethanol concentration of >20 g/L, a COuptake of >3.0 mmol/min, and a hydrogen uptake of >0.5 mmol/min. In theprocess of obtaining a high productivity steady state, the concentrationof CaCl₂.2H₂O was reduced to zero and ammonium concentration was loweredto 546 ppm.

Once the culture was at a high productivity steady state, the B, Mn andCu sources were eliminated from the medium preparation. Just prior toremoving those components, the culture conditions/parameters were asfollows:

Cell density—2.9 g/L

CO Conversion—86%

H₂Conversion—32%

CO Uptake—3.0 mmol/min

H₂ Uptake—0.54 mmol/min

Ethanol—21.8 g/L

Total Acetyl—2.7 g/L

Butanol—0.35 g/L

The culture parameters of gas uptake, H₂ and CO, product concentrationsand cell density were then monitored for any adverse affects. Ifremoving B, Cu and Mn did not affect those parameters after several (>3)cell retention times they were considered to be unnecessary to theculture

After ˜5.7 cell retention times (170 hours) the boron, copper andmanganese concentration in the culture broth had dropped to ˜0.41% ofthe beginning concentrations (0.0043 ppm B, 0.0006 ppm Cu, and 0.0068ppm Mn down from 1.05 ppm B, 0.149 ppm Cu and 1.67 ppm Mn). Theestimated remaining component concentrations in the broth weredetermined by washout calculations using a starting calciumconcentration, MFR, LRT and any additions of those components througheither the medium or spikes into the bioreactor. There were no adverseaffects on culture performance.

After 170 hours with no boron, copper and manganese addition, theculture parameters/condition were as follows:

Cell density—2.9 g/L

CO Conversion—86%

H₂Conversion—36%

CO Uptake—3.0 mmol/min

H₂ Uptake—0.61 mmol/min

Ethanol—21.0 g/L

Total Acetyl—2.9 g/L

Butanol—0.32 g/L

Example 2 Fermentation with Cobalt Limitations

Experiments were conducted in a bioreactor (New Brunswick BioFlo I orIIc) operated as a straight through CSTR, with no cell recycle loop.Bioreactor operating conditions were as follows:

Culture type was Clostridium ljungdahlii C01.

Culture temperature was kept at 37-39° C.

Agitation was 850 rpm on an analog readout (actual agitation was 931 rpmbased on a tachometer calibration curve).

The unroused culture volume was ˜1600-1650 ml.

Roused culture volume was ˜1950 ml.

The culture pH set point was 4.5. A solution of 7.7% NaHCO₃ was used forpH control.

Feed gas was a synthetic blend of 15% H₂, 45% N₂, 30% CO and 10% CO₂ fedto the culture at a rate of 286 ml/min.

Medium was fed into the reactor at ˜0.83 to ˜0.86 ml/min, or ˜1220ml/day.

Liquid and cell retention times were approximately 31-33 hours.

The medium used was as described below.

Component/ Conc in Med Ion Added As (ppm) NH₄ ⁺ NH₄Cl/(NH₄)₂HPO₄ 654  FeFeCl₂•4H₂O  16.8 Ni NiCl₂•6H₂O    0.198 Co CoCl₂•6H₂O 0-0.198 Se Na₂SeO₃   0.012 Zn ZnSO₄•7H₂O 0 Mo Na₂MoO₄•2H₂O 0 Mn MnCl₂•4H₂O 0 B H₃BO₃ 0 CuCuCl₂•2H₂O 0 W Na₂WO₄•2H₂O   1.12 K KCl  78.7 Mg MgCl₂•6H₂O  14.8 NaNaCl  0* Ca CaCl₂•2H₂O 0 Cysteine Cysteine HCl 250  HCl PO₄ ⁻²H₃PO₄/(NH₄)₂HPO₄ 279  Pantothenic Pantothenic Acid    0.0404 Acid BiotinBiotin    0.032 Thiamin Thiamine    0.080 *Na⁺ concentration is fromNaCl only. It does not include Na⁺ from the other components such asNa₂WO₄•2H₂O.

The bioreactor was operated until the culture obtained a highproductivity steady state. High productivity steady state was defined as˜2.5-3 g/L cell density, an ethanol concentration of >20 g/L, a COuptake of >3.0 mmol/min, and a hydrogen uptake of >0.5 mmol/min.

The culture parameters of gas uptake, H₂ and CO, product concentrationsand cell density were then monitored for any adverse affects. If thereduction in the component concentration did not affect those parametersafter several (>3) cell retention times, the concentration would bereduced further. If after a reduction in a component's concentration adrop in the culture parameters was seen, the concentration would beincreased back to a level that had previously shown to be adequate. Ifthe culture recovered, the concentration would be lowered again,sometimes to the same level as before to repeat the effect, sometime toa level somewhere in between what worked and what caused problems.

At the beginning of the experiment the cobalt concentration was atnormal medium levels, or 0.991 ppm. Culture parameters were stable at ˜3g/L cell density; 22-26 g/L ethanol; 2.7-3.7 g/L acetyl; 3.1 mmol/min COuptake; and 0.5-0.7 mmol/min H2 uptake. The cobalt was removed from themedium starting at t=0 hours. As the cobalt was washing out of thefermentor, there was only a slight drop in CO uptake from 3.1 to 2.9mmol/min. All other parameters remained more or less constant untilt=121 hrs. At that time the H₂ and CO uptake dropped to 0.16 and 2.6mmol/min respectively. The total acetyl also dropped quickly at thattime to 0.77 g/L indicating that the cobalt concentration had dropped toor below a limiting level. Cobalt washout calculations showed that bythe time the low cobalt level was affecting the culture parameters, thecobalt concentration in the reactor had dropped to 0.0222 ppm, or 2.24%of the original concentration. Cobalt was added into the reactor only,to raise the concentration to 23.3% of normal levels, or 0.231 ppm. Theeffect was immediately seen as an increase in CO uptake, H₂ uptake andacid concentration. No cobalt was added back into the medium at thistime to let the cobalt in the reactor to wash back down to limitinglevels once more. As seen previously, the culture parameters continuedto show no signs of distress until the cobalt had washed below 0.0220ppm. At t=210 hrs, the H₂ and CO uptakes as well as the acidconcentration had all dropped once again, showing the effects of cobaltlimitation. This time cobalt was added back to the reactor and medium at20% (0.198 ppm) in the medium and 21.2% (0.21 ppm) in the reactor. Asbefore, the effect was an immediate increase in both gas uptakes and inacid concentration.

The two different times the cobalt was washed out of the reactor untilthe culture showed signs of distress resulted in a cobalt concentrationof ˜0.022 ppm as limiting to the culture. When the cobalt concentrationwas then set at 0.023 ppm, the culture performed well with no adverseeffects. Based on that cobalt concentration the calculated parametersused to better correlate nutrient addition verses culture performancewere as follows: The mg of cobalt added per mmol of gas uptake was 0.005(mg/mmol). The μg of cobalt added per gram of cells produced was ˜9(μg/g).

Recovery from a cobalt limitation was rapid with no lasting adverseeffects. No permanent harm was done to the culture if cobalt wasincreased before the parameters drop to the point of secondary problems,i.e. gas toxicity or no acid present.

Dropping cobalt levels did cause the cell concentration to drop. Therewas no clear correlation between cobalt limitation and butanolproduction. Both CO and H2 conversion/uptake were affected by cobaltlimitation, but there was little to no effect seen until the cobaltconcentration in the culture dropped to ˜0.022 ppm or lower. There wasno gradual drop in gas conversion. However, once the cobaltconcentration dropped past the limitation point both CO and H₂conversions dropped very quickly. Once the CO and H₂ conversions beganto drop, the culture was already past the critical cobalt concentration,and cobalt must be added quickly in order to recover the culture. Anearlier indicator of cobalt limitation was the shift from acid toethanol in the product ratio. The acid concentration began to drop andthe ethanol concentration began to increase even before the dropping gasconversions were seen.

Example 3 Fermentation with Nickel Limitations

Experiments were conducted in a bioreactor (New Brunswick BioFlo I orIIc) operated as a straight through CSTR, with no permeate purge.Bioreactor operating conditions were as follows:

Culture type was Clostridium ljungdahlii C01

Culture temperature was kept at 37-39° C.

Agitation was 700 rpm on an analog readout.

The unroused culture volume was ˜1500-1650 ml.

Roused culture volume was ˜1900 ml.

The culture pH set point was 4.5. A solution of 7.7% NaHCO₃ was used farpH control.

Feed gas was a synthetic blend of 15% H₂, 45% N₂, 30% CO and 10% CO₂ fedto the culture at a rate of 290 ml/min.

Medium was fed into the reactor at ˜0.86 to ˜0.88 ml/min, or ˜1250ml/day.

Liquid and cell retention times were approximately 27-31 hours.

The medium used was as described below.

Component/ Conc in Med Ion Added As (ppm) NH₄ ⁺ NH₄Cl/(NH₄)₂HPO₄ 655  FeFeCl₂•4H₂O   8.4 Ni NiCl₂•6H₂O 0.0198-0.099 Co CoCl₂•6H₂O    0.0991 SeNa₂SeO₃    0.0116 Zn ZnSO₄•7H₂O 0 Mo Na₂MoO₄•2H₂O 0 Mn MnCl₂•4H₂O 0 BH₃BO₃ 0 Cu CuCl₂•2H₂O 0 W Na₂WO₄•2H₂O   1.12 K KCl  78.7 Mg MgCl₂•6H₂O 14.8 Na NaCl  0* Ca CaCl₂•2H₂O  0** Cysteine HCl Cysteine HCl 250  PH₃PO₄/(NH₄)₂HPO₄  31.8 Pantothenic Acid Pantothenic Acid     0.01515Biotin Biotin    0.0120 Thiamin Thiamine    0.0300 *Na⁺ concentration isfrom NaCl only. It does not include Na⁺ from the other components suchas Na₂WO₄•2H₂O. **Ca⁺² concentration does not include calcium frompantothenic acid, calcium salt.

The bioreactor was operated until the culture obtained a highproductivity steady state. High productivity steady state was defined as˜2.5-3 g/L cell density, an ethanol concentration of >20 g/L, a COuptake of >3.0 mmol/min, and a hydrogen uptake of >0.5 mmol/min.

The culture parameters of gas uptake, H₂ and CO, product concentrationsand cell density were then monitored for any adverse affects. If thereduction in the component concentration did not affect those parametersafter several (>3) cell retention times, the concentration would bereduced further. If after a reduction in a component's concentration adrop in the culture parameters was seen, the concentration would beincreased back to a level that had previously shown to be adequate. Ifthe culture recovered, the concentration would be lowered again,sometimes to the same level as before to repeat the effect, sometime toa level somewhere in between what worked and what caused problems.

At the start of this experiment the Ni concentration in the reactor haddropped to 56% of the original Ni level, or 0.11 ppm. Nickelconcentrations in the reactor were based on “washout” calculations thatused Ni concentration in the medium, Ni additions to the medium and/orreactor, and the liquid flows through the system to calculate thechanging Ni concentration in the reactor with time. As the Ni continuedto wash out of the reactor the culture parameters did not change. Celldensity remained ˜2.8 g/L; CO uptake was ˜3.2 mmol/min; H₂ uptake was˜0.7 mmol/min; ethanol concentration was 24 g/L; and the total acetyllevel was ˜2.5 g/L. However, by about t=107 hours the cell morphologyhad started to worsen. The percentage of long cells had increased from˜5% to 5-10% and the length of the long cells was increasing. The longcells were now showing some warping. The overall length of the averagecells was also increasing but with only mild or no warping. The Niconcentration in the reactor had dropped to 0.0996 ppm around the timethe cell morphology declined.

The nickel concentration in the reactor washed out to 50%, 0.0988 ppm,by t=˜160 hrs. As before, the culture parameters did not vary much.However, the cell morphology was worse when observed around t=250 hrs.The percentage of long cells had increased to 10-20% along with thedegree of bending or warping of those long cells. The remainder of theculture was average to slightly long in length with occasional mildbending. There were no severely bent cells, like coils or springs, butthere were several grainy cells and hollow bodied cells seen. Again, nochange to the culture parameters or nickel concentration was made.

The nickel concentration in the reactor remained at 50%, or 0.0988 ppm,until t=1885 hours. With a medium flow rate of ˜0.87 ml/min, the nickelfeed rate was 0.12 mg/day. Culture parameters were fairly constant at˜2.8 g/L cell density, ˜3.2 mmol/min CO uptake, ˜0.7 mmol/min H₂ uptake,˜25 g/L ethanol, ˜2.5 g/L total acetyl, and ˜0.3 g/L butanol. At the 50%nickel feed rate, Ni was added at ˜34 μg per gram of cells produced,˜0.022 μg per mmol of gas uptake. The cell morphology did not continueto worsen once the Ni concentration was 0.0988 ppm. It remained ˜10%long cells with mild warping, ˜5% very long cells with moderate warping,and the remainder of the cells was average to slightly long in lengthwith occasional warping.

At t=445 hrs, the Ni concentration in the medium was reduced to 25% ofthe original, or 0.049 ppm. Almost immediately a slow but steady changeto the culture parameters was observed. The CO uptake remained constantat ˜3.2 mmol/min, but the H₂ uptake started to decrease from 0.7-0.8mmol/min to 0.6-0.7 mmol/min within ˜120 hours of the Ni reduction. Theethanol concentration started to drop from ˜24 g/L to ˜21 g/L, and thetotal acetyl level also started to drop from ˜2.5 g/L to ˜2.0 g/L within˜160 hours of the Ni change. The butanol concentration started a slowbut steady increase almost as soon as the Ni was lowered in the medium.The concentration had increased from ˜0.21 g/L to ˜0.34 g/L by ˜635hours after Ni was lowered. The cell morphology was relativelyunchanged. The lower Ni feed rate was now 0.062 mg/day. At that feedrate Ni was added at ˜18 μg per gram of cells produced, ˜0.011 μg permmol of gas uptake.

To speed the effect of a low Ni concentration on the culture, the Nilevel in the medium was dropped to 10% or the original concentration, or0.0198 ppm, at t=638 hrs. The same trends in the culture parameterscontinued as before but at a faster rate. The H₂ uptake and acidconcentration continued to decrease. The cell density and CO uptake didnot change, and the butanol concentration continued to rise. There wasstill no change in cell density as it remained ˜2.8 g/L. Hydrogen uptakewas ˜0.5-0.6 mmol/min. Carbon monoxide uptake was still ˜3.2 mmol/min.The product concentrations were ˜21 g/L ethanol, ˜1.5 g/L total acetyl,and ˜0.65 g/L butanol. The Ni concentration was kept at 10% for anadditional 86 hours to determine a longer term affect on parameters andcell morphology. There was no further decline in culture parameters.Culture morphology did worsen somewhat showing an increase in the numberof long cells as well as an increase in the overall length of the cells.Approximately 10-15% of the cells were classified as long with warping.The remainder of the cells was short to slight long with the majority ofthe cells an average length and no warping. With the 10%, or 0.01975ppm, Ni concentration in the medium, the Ni feed rate was 0.025 mg/day.This provided ˜7 μg of Ni added per gram of cells produced, or ˜0.0048μg of Ni added per mmol of gas uptake. At t=2270 hours, the nickelconcentration was increased back to 50%, or 0.0988 ppm. Hydrogen uptakeincreased to ˜0.7 mmol/min. The CO uptake remained ˜3.2 mmol/min.Ethanol rose to ˜24 g/L. Acid increased to ˜2.5 g/L. Butanol dropped to˜0.24 g/L, and the cell density remained unchanged at ˜2.9 g/L. Cellmorphology also improved showing an overall decrease in the length ofcells as well as the number of long cells. Approximately 5-10% of thecells were classified as long with mild warping. The rest of the cellswere short to slightly long in length with most of them an averagelength with only occasional mild warping.

Decreasing the Ni concentration in the reactor to 0.0988 ppm, or 50%,caused no discernable change in the culture parameters. However, thecell morphology did worsen showing an increase in the overall length ofthe culture where up to 20% of the cells were considered long with mildto moderate warping. The cell morphology did not continue to worsenwhile at 50% Ni concentration showing that the culture would hold atsteady state under that condition.

When the nickel concentration in the medium was dropped to 25% ofnormal, or 0.049 ppm, the ethanol and total acetyl concentration and theH₂ uptake all started to drop. At the same time, the butanolconcentration started to increase slowly. These were all indicationsthat the culture was Ni limited, but the cell morphology remainedrelatively unchanged.

Based on the calculated nickel concentration in the reactor as theculture parameters and cell morphology started to decline, themorphology was the first to worsen as the Ni washed out down to 50%, or0.099 ppm. As the Ni concentration dropped further to 36%, or 0.072 ppm,the butanol concentration worsened. At 29% Ni, or 0.057 ppm, the H₂uptake started to drop. Then finally at 25% Ni, or 0.050 ppm, theethanol and acid concentrations started to decline. At 50% Ni only theculture morphology was affected. Once the Ni level dropped further,culture uptake and productivity declined. This signifies that a 50% Niconcentration in the medium, or a 0.12 mg/day feed rate, was very closeto the Ni limitation. Based on the culture parameters and the 0.12mg/day Ni feed rate, the Ni was added at ˜34 μg per gram of cellsproduced, ˜0.022 μg per mmol of gas uptake.

Signs of Ni limitation were decreased H₂ uptake, decreased acid level,and increased butanol followed by a decreased ethanol concentration.There was no change in cell density seen. Eventually cell morphology wasaffected showing an increase in the total number of long cells and theoverall length of those long cells. In general, as the length of thecells increased, the cell becomes more bent or warped.

Example 4 Fermentation with Tungsten Limitations

Experiments were conducted in a bioreactor (New Brunswick BioFlo I orIIc) operated as a straight through CSTR, with no permeate purge.Bioreactor operating conditions were as follows:

Culture type was Clostridium ljungdahlii C01.

Culture temperature was kept at 38-39° C.

Agitation was 700 rpm on an analog readout.

The unroused culture volume was ˜1550-1700 ml.

Roused culture volume was ˜1900 ml.

The culture pH set point was 4.5. A solution of 7.7% NaHCO₃ was used forpH control.

Feed gas was a synthetic blend of 15% H₂, 45% N₂, 30% CO and 10% CO₂ fedto the culture at a rate of 290 ml/min.

Medium was fed into the reactor at ˜0.86 to ˜0.88 ml/min, or ˜1250ml/day.

Liquid and cell retention times were approximately 28-31 hours.

The medium used was as described below.

Component/ Conc in Med Ion Added As (ppm) NH₄ ⁺ NH₄Cl/(NH₄)₂HPO₄ 655  FeFeCl₂•4H₂O   8.4 Ni NiCl₂•6H₂O 0.099-0.118 Co CoCl₂•6H₂O    0.0991 SeNa₂SeO₃    0.0116 Zn ZnSO₄•7H₂O 0 Mo Na₂MoO₄•2H₂O 0 Mn MnCl₂•4H₂O 0 BH₃BO₃ 0 Cu CuCl₂•2H₂O 0 W Na₂WO₄•2H₂O   0-0.56 K KCl  78.7 Mg MgCl₂•6H₂O 14.8 Na NaCl  0* Ca CaCl₂•2H₂O  0** Cysteine Cysteine HCl 250  HCl PH₃PO₄/(NH₄)₂HPO₄ 31.8-60   Pantothenic Pantothenic Acid     0.01515 AcidBiotin Biotin    0.0120 Thiamin Thiamine    0.0300 *Na⁺ concentration isfrom NaCl only. It does not include Na⁺ from the other components suchas Na₂WO₄•2H₂O. **Ca⁺² concentration does not include calcium frompantothenic acid, calcium salt.

The bioreactor was operated until the culture obtained a highproductivity steady state. High productivity steady state was defined as˜2.5-3 g/L cell density, an ethanol concentration of >20 g/L, a COuptake of >3.0 mmol/min, and a hydrogen uptake of >0.5 mmol/min.

The culture parameters of gas uptake, H₂ and CO, product concentrationsand cell density were then monitored for any adverse affects. If thereduction in the component concentration did not affect those parametersafter several (>3) cell retention times, the concentration would bereduced further. If after a reduction in a component's concentration adrop in the culture parameters was seen, the concentration would beincreased back to a level that had previously shown to be adequate. Ifthe culture recovered, the concentration would be lowered again,sometimes to the same level as before to repeat the effect, sometime toa level somewhere in between what worked and what caused problems.

During phosphorus testing, tungsten was removed from the medium at t=0hours. The culture was not recovering as anticipated during thephosphorus testing despite the addition of P back into the reactor andmedium preparation. When a series of attempts to improve the culturefailed, as a last resort tungsten was added back to the reactor at a 50%or normal level, or 0.56 ppm, at t=812 hours by adding 8 ml of a 0.2 g/lNa₂WO₄.2H₂O solution to 1.6 liters of culture. Tungsten washoutcalculations showed that the tungsten level in the reactor had washedout to <0.0001 ppm. Upon addition of tungsten, the culture respondedalmost immediately. The H₂ uptake started increasing. With the improvedH₂ conversions the feed gas flow rate was increased back to the originalsetting of ˜290 ml/min, by t=885 hours. That increased the CO and H₂uptakes back to 3.2 and ˜0.75 mmol/min respectively. With the increasedgas uptake the cell density increased to ˜2.7 g/L, and the ethanol levelrose to ˜22 g/L. The total acetyl and butanol levels remained about thesame at ˜3.5 and ˜0.45 g/L respectively. Another change in the culturewas an improvement in the cell morphology. With the tungsten addition,the overall cell length dropped significantly and there was less bendingand warping of the cells.

No tungsten was added back to the medium in order to wash the level inthe reactor back down in order to try and determine the level oftungsten required by the culture. As the tungsten was washing out the H₂uptake started to trend down around t=904 hours. No tungsten was addedto either reactor or medium. Around t=981 hours the butanolconcentration started to slowly increase. Then around t=1030 hours theethanol concentration started to drop. Still no tungsten was added. Byt=1100 hours H₂ uptake was ˜0.2 mmol/min; ethanol was ˜17 g/L; andbutanol was ˜0.74 g/L. The CO uptake had not been affected, and the celldensity was about the same.

At t=1100 hours tungsten was added to the reactor at 50% of normal or0.56 ppm. As seen before, the culture started to improve almostimmediately. The H₂ uptake started to increase; ethanol concentrationrose; the acid level dropped; cell density increased slightly; and thebutanol concentration started to decrease. By the end of the reportingperiod the cell density was ˜3.3 g/L; CO and H₂ uptakes were ˜3.2 and˜0.75 mmol/min respectively; ethanol was 22 g/L; acid was ˜2.5 g/L; andbutanol was 0.52 g/L. The tungsten level in the reactor had washed backdown to 0.045 ppm, or 4.0% of original concentration, by the end of thereporting period.

The tungsten limitation was about 2.7% of the original concentrationpreviously added, or 0.030 ppm. The culture first started showing signsof distress as a decreasing H₂ uptake when the tungsten had washed backout of the reactor down to 0.030 ppm. At that concentration tungsten wasadded at 10 μg per gram of cells produced, 0.0068 μg per mmol of gasuptake.

Example 5 Fermentation with Boron, Copper, Manganese and MolybdenumLimitations

A New Brunswick Bioflow Cellii Gen 115 reactor containing a medium whichdid not include any B, Cu, Mn or Mo (designated medium A) or a knownmedia (designated 402 medium) which included B, Cu, Mn and Mo wasinoculated with 0.39 g/L of actively growing Clostridium ljungdahliiCO-1 strain.

After, the inoculation the rate of agitation of the reactor was set to800 rpm. Gas and liquid samples taken from the reactor at approximately1 hour intervals were analyzed for consumption or production of variousgas components, broth acetic acid concentration, broth ethanolconcentration and the optical density of the culture. Also thecomposition of various gases in the syngas was measured daily and thesyngas flow to the reactor was measured real time by the mass flowcontroller regulating syngas to the reactor. The actual gas flow wascalculated using the equation obtained by calibrating the mass flowcontroller. Calculations were conducted to determine the necessary rateof gas flow to the reactor to maintain a constant percentage of H₂uptake from the H₂ in the inflow gas to the reactor or in another words,in this particular experiment, rate of gas flowing into the reactor wasmaintain so that culture uptake of H₂ is 4.5% of the total molecules ofgas flowing into the reactor. Then the reactor was supplied with gas atthe rate calculated above (to keep the percentage of uptake of H₂ fromthe inlet to 4.5% of total gas molecules).

For all three experiments, the cell recycle system was attached to thereactor before inoculation and had media circulating through the systemfor the entire duration of the experiment. For the first experiment withmedium A, at 2.75 hours after the inoculation (after CO conversions hadreached 80% or above), media flow to the reactor was started at 1.0ml/min and permeate was drawn out from the reactor at 1.0 ml/min. At6.83 hours after the inoculation, the media flow to the reactor wasincreased to 2.0 ml/min and permeate was drawn out from the reactor at2.0 ml/min.

For the second experiment with the 402 medium, at 1.9 hours after theinoculation (after CO gas conversions had reached 80% or above), themedia flow to the reactor was started at 2.0 ml/min and permeate wasdrawn out from the reactor at 2.0 ml/min.

For the third experiment with medium A, at 2.0 hours after theinoculation (after CO gas conversions had reached 80% or above), themedia flow to the reactor was started at 2.0 ml/min and permeate wasdrawn out from the reactor at 2.0 ml/min. For all three experiments,introduction of cell recycle system was applied to remove rapid build upof ethanol in the reactor.

Medium A and the 402 medium provided close to equal performances forhydrogen uptake with C. ljungdahlii.

Example 6 Fermentation with Molybdenum Limitations

Experiments were conducted in a bioreactor (New Brunswick BioFlo I orIIc) operated as a straight through CSTR, with no permeate purge.Bioreactor operating conditions were as follows:

Culture type was Clostridium ljungdahlii C01.

Culture temperature was kept at 38-39° C.

Agitation was 850 rpm on an analog readout.

The unroused culture volume was ˜1600-1650 ml.

Roused culture volume was ˜1900 ml.

The culture pH set point was 4.5. A solution of 7.7% NaHCO₃ was used forpH control.

Feed gas was a synthetic blend of 15% H₂, 45% N₂, 30% CO and 10% CO₂ fedto the culture at a rate of 282 ml/min.

Medium was fed into the reactor at ˜0.88 ml/min, or ˜1300 ml/day.

Liquid and cell retention times were approximately 29-31 hours.

The medium used was as described below.

Component/ Conc in Med Ion Added As (ppm) NH₄ ⁺ NH₄Cl/(NH₄)₂HPO₄ 546  FeFeCl₂•4H₂O  16.8 Ni NiCl₂•6H₂O    0.1975 Co CoCl₂•6H₂O    0.991 SeNa₂SeO₃    0.0456 Zn ZnSO₄•7H₂O    0.455 Mo Na₂MoO₄•2H₂O 0 Mn MnCl₂•4H₂O0 B H₃BO₃ 0 Cu CuCl₂•2H₂O 0 W Na₂WO₄•2H₂O   1.12 K KCl  78.6 MgMgCl₂•6H₂O  29.9 Na NaCl   78.7* Ca CaCl₂•2H₂O  0** Cysteine HClCysteine HCl 250  P H₃PO₄/(NH₄)₂HPO₄ 279  *Na⁺ concentration is fromNaCl only. It does not include Na⁺ from the other components such asNa₂WO₄•2H₂O. **Ca⁺² concentration does not include calcium frompantothenic acid, calcium salt.

The bioreactor was operated until the culture obtained a highproductivity steady state. High productivity steady state was defined as˜2.5-3 g/L cell density, an ethanol concentration of >20 g/L, a COuptake of >3.0 mmol/min, and a hydrogen uptake of >0.5 mmol/min.

The culture parameters of gas uptake, H₂ and CO, product concentrationsand cell density were then monitored for any adverse affects. If thereduction in the component concentration did not affect those parametersafter several (>3) cell retention times, the concentration would bereduced further. If after a reduction in a component's concentration adrop in the culture parameters was seen, the concentration would beincreased back to a level that had previously shown to be adequate. Ifthe culture recovered, the concentration would be lowered again,sometimes to the same level as before to repeat the effect, sometime toa level somewhere in between what worked and what caused problems.

Molybdenum requirement testing was started at t=0 hours by eliminatingNa₂MoO₄.2H₂O from the medium preparation. Just prior to removing thosecomponents, the culture conditions I parameters were as follows:

Cell density—3.2 g/L

CO Conversion—86%

H₂Conversion—36%

CO Uptake—3.0 mmol/min

H₂ Uptake—0.56 mmol/min

Ethanol—21.8 g/L

Total Acetyl—2.3 g/L

Butanol—0.32 g/L

After ˜9.7 cell retention times (292 hours) the molybdenum concentrationin the culture broth had dropped to <0.0001% of the beginningconcentration of 0.238 ppm Mo. The estimated remaining componentconcentrations in the broth were determined by washout calculationsusing a starting calcium concentration, MFR, LRT and any additions of Mothrough either the medium or spikes into the bioreactor. There were noadverse affects on culture performance. After 292 hours with nomolybdenum addition, the culture parameters/condition were as follows:

Cell density—2.9 g/L

CO Conversion—86%

H₂Conversion—36%

CO Uptake—3.0 mmol/min

H₂ Uptake—0.61 mmol/min

Ethanol—21.0 g/L

Total Acetyl—2.9 g/L

Butanol—0.32 g/L

Example 7 Fermentation with Magnesium Limitations

Experiments were conducted in a bioreactor (New Brunswick BioFlo I orIIc) operated as a straight through CSTR, with no cell recycle loop.Bioreactor operating conditions were as follows:

Culture type was Clostridium ljungdahlii C01.

Culture temperature was kept at 37-39° C.

Agitation was 880-890 rpm on an analog readout.

The unroused culture volume was ˜1275 ml.

Roused culture volume was ˜1900 ml.

The culture pH set point was 4.2. A solution of 7.7% NaHCO₃ was used forpH control.

Feed gas was a synthetic blend of 15% H₂, 45% N₂, 30% CO and 10% CO₂ fedto the culture at a rate of 232 ml/min.

Medium was fed into the reactor at ˜0.70 ml/min, or ˜1008 ml/day.

Liquid and cell retention times were approximately 29-31 hours.

The medium used was as described below.

Component/ Conc in Med Ion Added As (ppm) NH₄ ⁺ NH₄Cl/(NH₄)₂HPO₄ 838 FeFeCl₂•4H₂O 16.8 Ni NiCl₂•6H₂O 0.198 Co CoCl₂•6H₂O 0.991 Se Na₂SeO₃0.0913 Zn ZnSO₄•7H₂O 0.455 Mo Na₂MoO₄•2H₂O 0.238 Mn MnCl₂•4H₂O 0.167 BH₃BO₃ 1.05 Cu CuCl₂•2H₂O 0.149 W Na₂WO₄•2H₂O 1.12 K KCl 78.6 MgMgCl₂•6H₂O 7.47-14.9 Na NaCl 78.7* Ca CaCl₂•2H₂O 0 Cysteine HCl CysteineHCl 250 PO₄ ⁻² H₃PO₄/(NH₄)₂HPO₄ 816 Pantothenic Acid Pantothenic Acid0.0505 Biotin Biotin 0.0400 Thiamin Thiamine 0.1000 Na⁺ concentration isfrom NaCl only. It does not include Na⁺ from the other components suchas Na₂WO₄•2H₂O.

The bioreactor was operated until the culture obtained a highproductivity steady state. High productivity steady state was defined as˜2.5-3 g/L cell density, an ethanol concentration of >20 g/L, a COuptake of >3.0 mmol/min, and a hydrogen uptake of >0.5 mmol/min.

The culture parameters of gas uptake, H₂ and CO, product concentrationsand cell density were then monitored for any adverse affects. If thereduction in the component concentration did not affect those parametersafter several (>3) cell retention times, the concentration would bereduced further. If after a reduction in a component's concentration adrop in the culture parameters was seen, the concentration would beincreased back to a level that had previously shown to be adequate. Ifthe culture recovered, the concentration would be lowered again,sometimes to the same level as before to repeat the effect, sometime toa level somewhere in between what worked and what caused problems.

At the beginning of the experiment the magnesium concentration was atnormal ethanol medium levels, or 59.77 ppm. Culture parameters werestable at ˜3.1 g/L cell density; 20.5 g/L ethanol; 3.0 g/L acetyl; 2.4mmol/min CO uptake; and 0.42 mmol/min H₂ uptake. The magnesiumconcentration was decreased to 14.97 ppm in the medium starting at t=0hours. As the magnesium was washing out of the fermentor, all parameterswere monitored for potential effects on culture performance. After ˜300hours or ˜10 cell retention times, there was no observed detrimentaleffects on culture performance. There was an almost immediate drop inacetyl concentration after the decrease in magnesium, but this was dueto a medium feed problem. Once the problem was corrected, the acetylconcentration increased back to levels similar to those seen when Mgconcentration was at 59.77 ppm. It was concluded that a medium feedcontaining 14.97 ppm Mg was able to sustain a culture at ˜3 g/L celldensity at a ˜30 hour cell retention time.

Mg at 59.77 ppm

Cell density—3.1 g/L

CO Conversion—84%

H₂Conversion—32%

CO Uptake—2.4 mmol/min

H₂ Uptake—0.42 mmol/min

Ethanol—20.5 g/L

Total Acetyl—2.4 g/L

Mg at 14.94 ppm

Cell density—3.0 g/L

CO Conversion—84%

H₂Conversion—34%

CO Uptake—2.4 mmol/min

H₂ Uptake—0.45 mmol/min

Ethanol—21.0 g/L

Total Acetyl—2.7 g/L

The magnesium concentration was decreased further to 7.47 ppm in themedium starting at t=403 hours. As the magnesium was washing out of thefermentor, all parameters were monitored for potential effects onculture performance. After only 20 hours the hydrogen conversion anduptake began to decrease. The calculated Mg concentration in the culturewas ˜11 ppm. The culture performance continued to decline with droppingCO conversions/uptake, increasing acetyl concentration, decreasingethanol concentration and a steady drop in cell density despite severaladditions of magnesium to both the culture and medium. The culture waseventually lost. It was concluded that a medium feed containing 7.47 ppmMg was not sufficient to sustain a 3 g/l culture at a 30 hour cellretention time.

Example 8 Fermentation with Potassium Limitations

Experiments were conducted in a bioreactor (New Brunswick BioFlo I orIIc) operated as a straight through CSTR, with no cell recycle loop.Bioreactor operating conditions were as follows:

Culture type was Clostridium ljungdahlii C01.

Culture temperature was kept at 38-39° C.

Agitation was 950-1000 rpm on an analog readout.

Roused culture volume was ˜1550 ml.

The culture pH set point was 4.2. A solution of 7.5% NaHCO₃ was used forpH control.

Feed gas was a synthetic blend of 15% H₂, 45% N₂, 30% CO and 10% CO₂ fedto the culture at a rate of 279 ml/min.

Medium was fed into the reactor at ˜0.80-0.85 ml/min, or ˜1220 ml/day.

Liquid and cell retention times were approximately 28-30 hours.

The medium used was as described below.

Component/ Conc in Med Ion Added As (ppm) NH₄ ⁺ NH₄Cl/(NH₄)₂HPO₄ 838  FeFeCl₂•4H₂O  16.8 Ni NiCl₂•6H₂O    0.198 Co CoCl₂•6H₂O    0.991 SeNa₂SeO₃    0.0456 Zn ZnSO₄•7H₂O    0.455 Mo Na₂MoO₄•2H₂O 0 Mn MnCl₂•4H₂O0 B H₃BO₃ 0 Cu CuCl₂•2H₂O 0 W Na₂WO₄•2H₂O   1.12 K KCl 39.3-118 MgMgCl₂•6H₂O  59.8 Na NaCl  0* Ca CaCl₂•2H₂O 0 Cysteine HCl Cysteine HCl250  PO₄ ⁻² H₃PO₄/(NH₄)₂HPO₄ 816  Pantothenic Acid Pantothenic Acid   0.0151 Biotin Biotin    0.012 Thiamin Thiamine    0.030 *Na⁺concentration is from NaCl only. It does not include Na⁺ from the othercomponents such as Na₂WO₄•2H₂O.

The bioreactor was operated until the culture obtained a highproductivity steady state. High productivity steady state was defined as˜2.5-3 g/L cell density, an ethanol concentration of >20 g/L, a COuptake of >3.0 mmol/min, and a hydrogen uptake of >0.5 mmol/min.

The culture parameters of gas uptake, H₂ and CO, product concentrationsand cell density were then monitored for any adverse affects. If thereduction in the component concentration did not affect those parametersafter several (>3) cell retention times, the concentration would bereduced further. If after a reduction in a component's concentration adrop in the culture parameters was seen, the concentration would beincreased back to a level that had previously shown to be adequate. Ifthe culture recovered, the concentration would be lowered again,sometimes to the same level as before to repeat the effect, sometime toa level somewhere in between what worked and what caused problems.

At the beginning of the experiment the potassium concentration was atnormal ethanol medium levels, or 78.7 ppm. Culture parameters werestable at ˜3 g/L cell density; ˜22 g/L ethanol; ˜2.6 g/L acetyl; 0.5 g/Lbutanol; 3.1 mmol/min CO uptake; and 0.5-0.6 mmol/min H₂ uptake. Thepotassium was reduced to 39.3 ppm in the medium starting at t=0 hours.As the potassium was washing out of the fermentor, the cultureparameters were monitored for changes. After approximately 30 hours, theH₂ uptake began to drop followed by a drop in CO uptake. Hydrogen uptakedropped to 0.078 mmol/min and CO uptake dropped to a low of 2.8mmol/min. The acetic acid concentration also decreased to a low of 0.78g/L approximately 40 hours after the potassium reduction followed by adrop in ethanol concentration to 19.2 g/L. Butanol concentrationsincreased to 0.67 g/L. Cell density was also affected as seen by adecrease to 2.3 g/L, but that may have been the result of anunintentional cell retention time decrease to 27 hours immediately afterthe drop in potassium. Potassium was added into the reactor to raise theconcentration to 78.7 ppm. The effect was immediately seen as anincrease in CO uptake, H₂ uptake, ethanol and acid concentration.Butanol levels slowly decreased back down to ˜0.53 g/L with the increasein potassium.

Once the culture had seemed to recover back to levels observed beforepotassium was limited, the potassium concentration in the medium wasdropped to 59.0 ppm at t=139 hours. Again, culture parameters weremonitored for any changes. As before the H₂ uptake began to decrease ˜8hours after the reduction of potassium. However, this time the CO uptakewas not affected. There was a small increase in butanol to ˜0.57 g/L.There was a drop in acetic acid concentration, but this was acontinuation of a decreasing trend that was seen before the drop inpotassium levels. Ethanol levels remained ˜22 g/L. Cell density showed asmall drop with the decrease in potassium levels from approximately 3.0g/L to 2.8 g/L. The scatter in the data allowed for only approximatecell density concentrations to be reported. Potassium was added into thereactor to raise the concentration to 78.7 ppm. The effect wasimmediately seen as an increase in H₂ uptake, ethanol concentration,acid concentration and cell density confirming that the culture waspotassium limited.

The overall effect of dropping potassium to 59.0 ppm was smaller than itwas dropped to 39.3 ppm, but that level was still considered limiting. Apotassium level of 78.7 ppm in the medium was therefore considered closeto limiting. To determine if that level was indeed limiting, thepotassium concentration in the medium was increased to 98.3 ppm at t=243hours. With the increase in potassium, the H₂ uptake rose from ˜0.61mmol/min to ˜0.71 mmol/min. There was also an increase in cell densityfrom ˜3.0 to ˜3.3 g/l. Acetic acid was higher at ˜3.3 g/L as compared to2.6 when potassium was at 78.7 ppm. Butanol concentrations were more orless constant within the scatter of the data. Ethanol levels seemed toshow a small increase to 24 g/l, but the scatter of the data made itdifficult to determine. Since there was some positive effects fromincreasing the potassium to 98.3 ppm, the potassium concentration wasincreased further to 118 ppm at t=375 hours. The only definitive effectseen on culture parameters was a further cell density increase to ˜3.9g/L. All other parameters remained constant within the scatter of thedata.

Example 9 Fermentation with Cysteine Limitations

Experiments were conducted in a bioreactor (New Brunswick BioFlo I orIIc) operated as a straight through CSTR, with no cell recycle loop.Bioreactor operating conditions were as follows:

Culture type was Clostridium ljungdahlii C01.

Culture temperature was kept 38-39° C.

Agitation was 900 rpm on an analog readout.

Roused culture volume was ˜1650 ml.

The culture pH set point was 4.5. A solution of 7.5% NaHCO₃ was used forpH control.

Feed gas was a synthetic blend of 15% H₂, 45% N₂, 30% CO and 10% CO₂ fedto the culture at a rate of 279 ml/min.

Medium was fed into the reactor at ˜0.83-0.86 ml/min, or ˜1220 ml/day.

Liquid and cell retention times were approximately 28-30 hours.

The medium used was as described below.

Component/ Conc in Med Ion Added As (ppm) NH₄ ⁺ NH₄Cl/(NH₄)₂HPO₄ 838  FeFeCl₂•4H₂O  16.8 Ni NiCl₂•6H₂O    0.198 Co CoCl₂•6H₂O    0.991 SeNa₂SeO₃    0.0456 Zn ZnSO₄•7H₂O    0.455 Mo Na₂MoO₄•2H₂O 0 Mn MnCl₂•4H₂O0 B H₃BO₃ 0 Cu CuCl₂•2H₂O 0 W Na₂WO₄•2H₂O   1.12 K KCl  78.7 MgMgCl₂•6H₂O  59.8 Na NaCl  0* Ca CaCl₂•2H₂O 0 Cysteine Cysteine HCl125-250 HCl PO₄ ⁻² H₃PO₄/(NH₄)₂HPO₄ 816  Pantothenic Pantothenic Acid   0.0353 Acid Biotin Biotin    0.028 Thiamin Thiamine    0.070 *Na⁺concentration is from NaCl only. It does not include Na⁺ from the othercomponents such as Na₂WO₄•2H₂O.

At the beginning of the experiment, the cysteine concentration was atnormal ethanol medium levels, or 250 ppm. Culture parameters were stableat ˜3 g/L cell density; 23 g/L ethanol; 2.4 g/L acetyl; 3.1 mmol/min COuptake; and 0.56 mmol/min H₂ uptake. The cysteine was decreased to 187.5ppm in the medium starting at t=0 hours. As the cysteine was washing outof the fermentor, all parameter was monitored for signs of limitation.The cysteine concentration was held at that level for 167 hours or 5XRTs. All parameters remained constant. A 187.5 ppm concentration ofcysteine was enough to sustain a 3 g/L culture with a 33 hours cellretention time.

The cysteine concentration was decreased further in the medium from187.5 ppm to 125 ppm at t=167 hours. Almost immediately, the H₂ uptakeand conversions began to drop along with a decreasing acetic acidconcentration. CO uptake and conversions and cell density were constant.The H₂ uptake dropped to 0.36 mmol/min, H₂ conversion dropped to 21% andacetic acid decreased to 1.7 g/L. Cysteine concentration in both themedium and bioreactor were increased to 187.5 ppm then 250 ppm. Theculture quickly recovered. A concentration of 125 ppm of cysteine wasnot sufficient to sustain a 3 g/L culture at a 33 hour cell retentiontime.

After the culture had fully recovered, the cysteine limitation wastested again. At t=407 hrs, the cysteine in the medium was dropped to162.5 ppm. As seen before, the H₂ conversions and uptake began droppingalmost immediately. The acetic acid concentration again dropped but notas quickly or as far as when the cysteine concentration was 125 ppm. TheH₂ uptake dropped to 0.49 mmol/min, H₂ conversion dropped to 29% andacetic acid decreased from 3.0 to 2.7 g/L. A concentration of 162.5 ppmof cysteine was not sufficient to sustain a 3 g/L culture at a 33 hourcell retention time.

Example 10 Fermentation with Thiamine Limitations

Experiments were conducted in a bioreactor (New Brunswick BioFlo I orIIc) operated as a straight through CSTR. Bioreactor operatingconditions were as follows:

Culture type was Clostridium ljungdahlii C01.

Culture temperature was kept at 38-39° C.

Agitation was 950 rpm on an analog readout.

Roused culture volume was ˜1950 ml.

The culture pH set point was 4.5. A solution of 7.5% NaHCO₃ was used forpH control.

Feed gas was a synthetic blend of 15% H₂, 45% N₂, 30% CO and 10% CO₂ fedto the culture at a rate of 279 ml/min.

Medium was fed into the reactor at ˜0.84-0.86 ml/min, or ˜1220 ml/day.

Liquid and cell retention times were approximately 30-32 hours.

The medium used was as described below

Component/ Conc in Med Ion Added As (ppm) NH₄ ⁺ NH₄Cl/(NH₄)₂HPO₄ 654  FeFeCl₂•4H₂O   8.4 Ni NiCl₂•6H₂O    0.198 Co CoCl₂•6H₂O    0.991 SeNa₂SeO₃    0.012 Zn ZnSO₄•7H₂O    0.455 Mo Na₂MoO₄•2H₂O 0 Mn MnCl₂•4H₂O0 B H₃BO₃ 0 Cu CuCl₂•2H₂O 0 W Na₂WO₄•2H₂O   1.12 K KCl  78.7 MgMgCl₂•6H₂O  14.8 Na NaCl  0* Ca CaCl₂•2H₂O 0 Cysteine HCl Cysteine HCl250  PO₄ ⁻² H₃PO₄/(NH₄)₂HPO₄ 384  Pantothenic Pantothenic Acid    0.283Acid Biotin Biotin    0.0070 Thiamin Thiamine    0.0105 *Na⁺concentration is from NaCl only. It does not include Na⁺ from the othercomponents such as Na₂WO₄•2H₂O.

The vitamin solution normally added to the medium was a solution of0.0505 g/L pantothenate, 0.040 g/L biotin and 0.10 g/L thiamine. Forthis study, the vitamin solution was separated into three solutions, onefor each component. The concentrations of those solutions were kept thesame as in the original vitamin mix. This way the concentration of eachcomponent could be adjusted as needed without changing the other vitaminconcentrations.

At the beginning of this experiment, the pantothenic acid concentrationin the medium was 0.03535 ppm or 0.7 ml of a 0.0505 g/L pantothenic acidsolution per liter of medium. The biotin concentration in the medium was25% of the normal vitamin concentration or 0.0070 ppm in the medium.This was the equivalent of 0.175 ml of the 0.04 g/L biotin solutionadded per liter of medium. The thiamine level in the medium was 25% ofthe normal vitamin concentration, or 0.0175 ppm. This was the equivalentof 0.175 ml of a 0.10 g/L thiamine solution added per liter of medium.At t=0 hrs, the thiamine concentration in the medium was dropped to 15%of normal, or 0.0105 ppm. There was no immediate effect seen on the celldensity. However, the H₂ uptake, total acetyl concentration, and ethanolconcentration all started to drop almost immediately indicating that theprevious thiamine concentration of 0.0175 ppm was already close tolimiting. At the same time the CO uptake increased slightly from 3.1 to3.2 mmol/min. This may be an indication of an increase in mass transferduring that time even though the agitation rate remained constant. Toverify the cause of the drop in culture productivity, 0.5 ml of thepantothenic acid solution was first added to the reactor at t=43 hrs.When this had no affect on the culture, 0.115 ml of the thiaminesolution was added back to the reactor at t=84 hrs to raise the thiaminelevel in the reactor to ˜0.0175 ppm. This had an immediate affect on theculture. Hydrogen uptake, acid levels, and ethanol concentration allstarted to increase. The culture needed the additional thiamine.

No further changes to the reactor were made in order to wash the addedpantothenic acid and thiamine out of the reactor back down to the 0.0354ppm pantothenic acid and 0.0105 ppm thiamine coming in from mediumaddition. Over the following 228 hrs as the vitamins washed out, the H₂uptake first increased to ˜0.53 mmol/min then dropped to a low of ˜0.31mmol/min supposedly as the extra pantothenate and thiamine washed backout of the reactor. However, with no changes to the vitamin levels orany other culture changes, the H₂ uptake started to steadily increasereaching ˜0.5 mmol/min around t=273 hrs. The acid and ethanolconcentrations did not follow a set pattern but varied around 25 g/Lethanol and 1.1-2.4 g/L acid. The CO uptake remained constant at 3.2mmol/min, and the cell density held fairly constant at 2.8-3.0 g/L.

At the beginning of the experiment when the thiamine level in the mediumwas dropped from 0.0175 ppm to 0.0105 ppm, the effect on the culture'sparameters was almost immediate indicating that the 0.0175 ppm thiaminelevel was close to limiting already. The calculated parameters used tobetter correlate nutrient addition verses culture performance before thedrop to 0.0105 ppm thiamine were as follows: The μg thiamine added permmol of gas uptake was 0.0041 μg/mmol. The μg of thiamine added per gramof cells produced was ˜6.5 μg/g. Further confirmation that the thiaminewas indeed limiting at 0.0105 ppm was the immediate improvement inculture parameters when the thiamine level in the reactor wastemporarily increased to 0.0175 ppm in the reactor.

While the invention herein disclosed has been described by means ofspecific aspects, examples and applications thereof, numerousmodifications and variations could be made thereto by those skilled inthe art without departing from the scope of the invention set forth inthe claims.

What is claimed is:
 1. A fermentation medium comprising: at least about112 mg of nitrogen per gram of cells, at least about 10.5 mg ofphosphorous per gram of cells, or at least about 26 mg of potassium pergram of cells, wherein the fermentation medium has a weight ratio of NH₄⁺ to B of about 625:1 or more, or a weight ratio of NH₄₊ to Mn of about4050:1 or more, or a weight ratio of NH₄ ⁺ to Mo of about 2500:1 ormore, or a ratio of NH₄₊ to Cu of about 4050:1 or more; or wherein thefermentation medium has a weight ratio of P to B of about 30:1 or more,or a weight ratio of P to Mn of about 190:1 or more, or a weight ratioof P to Mo of about 120:1 or more, or a weight ratio of P to Cu of about190:1 or more; or wherein the fermentation medium has a weight ratio ofK to B of about 35:1 or more, or a weight ratio of K to Mn of about245:1 or more, or a weight ratio of K to Mo of about 150:1 or more, or aweight ratio of K to Cu of about 245:1 or more.
 2. The fermentationmedium of claim 1 wherein the fermentation medium includes about 112 toabout 125 mg of nitrogen per gram of cells, about 10.5 to about 15 mg ofphosphorous per gram of cells, or about 26 to about 36 mg of potassiumper gram of cells.
 3. The fermentation medium of claim 2 wherein thenitrogen is provided from a nitrogen source selected from the groupconsisting of ammonium chloride, ammonium phosphate, ammonium sulfate,ammonium nitrate, and mixtures thereof, the phosphorous is provided froma phosphorous source selected from the group consisting of phosphoricacid, ammonium phosphate, potassium phosphate, and mixtures thereof, andthe potassium is provided from a potassium source selected from thegroup consisting of potassium chloride, potassium phosphate, potassiumnitrate, potassium sulfate, and mixtures thereof.
 4. The fermentationmedium of claim 1 wherein the fermentation medium includes one or moreof at least about 2.7 mg of iron per gram of cells, at least about 10 μgof tungsten per gram of cells, at least about 34 μg of nickel per gramof cells, at least about 9 μg of cobalt per gram of cells, at leastabout 4.5 mg of magnesium per gram of cells, at least about 11 mg ofsulfur per gram of cells, and at least about 6.5 μg of thiamine per gramof cells.
 5. The fermentation medium of claim 4 wherein the fermentationmedium includes one or more of about 2.7 to about 5 mg of iron per gramof cells, about 10 to about 30 μg of tungsten per gram of cells, about34 to about 40 μg of nickel per gram of cells, about 9 to about 30 μg ofcobalt per gram of cells, about 4.5 to about 10 mg of magnesium per gramof cells, about 11 to about 20 mg of sulfur per gram of cells, and about6.5 to about 20 μg of thiamine per gram of cells.
 6. The fermentationmedium of claim 4 wherein the iron is provided from an iron sourceselected from the group consisting of ferrous chloride, ferrous sulfate,and mixtures thereof, the tungsten is provided from a tungsten sourceselected from the group consisting of sodium tungstate, calciumtungstate, potassium tungstate, and mixtures thereof, the nickel isprovided from a nickel source selected from the group consisting ofnickel chloride, nickel sulfate, nickel nitrate, and mixtures thereof,the cobalt is provided from a cobalt source selected from the groupconsisting of cobalt chloride, cobalt fluoride, cobalt bromide, cobaltiodide, and mixtures thereof, the magnesium is provided from a magnesiumsource selected from the group consisting of magnesium chloride,magnesium sulfate, magnesium phosphate, and the sulfur is provided froma sulfur source selected from the group consisting of cysteine, sodiumsulfide, and mixtures thereof.
 7. The fermentation medium of claim 1wherein the fermentation medium has a pH of about 4.2 to about 4.8.
 8. Afermentation process comprising fermenting syngas in a fermentationmedium, the process effective for providing a specific STY of at leastabout 1 gram of ethanol/(L·day·gram cells), wherein the fermentationmedium has a weight ratio of NH₄₊ to B of about 625:1 or more, or aweight ratio of NH₄ ⁺ to Mn of about 4050:1 or more, or a weight ratioof NH₄ ⁺ to Mo of about 2500:1 or more, or a ratio of NH₄ ⁺ to Cu ofabout 4050:1 or more; or wherein the fermentation medium has a weightratio of P to B of about 30:1 or more, or a weight ratio of P to Mn ofabout 190:1 or more, or a weight ratio of P to Mo of about 120:1 ormore, or a weight ratio of Mn to Cu of about 190:1 or more; or whereinthe fermentation medium has a weight ratio of K to B of about 35:1 ormore, or a weight ratio of K to Mn of about 245:1 or more, or a weightratio of K to Mo of about 150:1 or more, or a weight ratio of K to Cu ofabout 245:1 or more.
 9. The fermentation process of claim 8 wherein thefermentation medium includes at least one or more of at least about 112mg of nitrogen per gram of cells, at least about 10.5 mg of phosphorousper gram of cells, or at least about 26 mg of potassium per gram ofcells.
 10. The fermentation process of claim 9 wherein the fermentationmedium includes at least one or more of about 112 to about 125 mg ofnitrogen per gram of cells, about 10.5 to about 15 mg of phosphorous pergram of cells, or about 26 to about 36 mg of potassium per gram ofcells.
 11. The fermentation process of claim 9 wherein the nitrogen isprovided from a nitrogen source selected from the group consisting ofammonium chloride, ammonium phosphate, ammonium sulfate, ammoniumnitrate, and mixtures thereof, the phosphorous is provided from aphosphorous source selected from the group consisting of phosphoricacid, ammonium phosphate, potassium phosphate, and mixtures thereof, andthe potassium is provided from a potassium source selected from thegroup consisting of potassium chloride, potassium phosphate, potassiumnitrate, potassium sulfate, and mixtures thereof.
 12. The fermentationprocess of claim 8 wherein the fermentation medium includes one or moreof at least about 2.7 mg of iron per gram of cells, at least about 10 μgof tungsten per gram of cells, at least about 34 μg of nickel per gramof cells, at least about 9 μg of cobalt per gram of cells, at leastabout 4.5 mg of magnesium per gram of cells, at least about 11 mg ofsulfur per gram of cells, and at least about 6.5 μg of thiamine per gramof cells.
 13. The fermentation process of claim 12 wherein thefermentation medium includes one or more of about 2.7 to about 5 mg ofiron per gram of cells, about 10 to about 30 μg of tungsten per gram ofcells, about 34 to about 40 μg of nickel per gram of cells, about 9 toabout 30 μg of cobalt per gram of cells, about 4.5 to about 10 mg ofmagnesium per gram of cells, about 11 to about 20 mg of sulfur per gramof cells, and about 6.5 to about 20 μg of thiamine per gram of cells.14. The fermentation process of claim 12 wherein the iron is providedfrom an iron source selected from the group consisting of ferrouschloride, ferrous sulfate, and mixtures thereof, the tungsten isprovided from a tungsten source selected from the group consisting ofsodium tungstate, calcium tungstate, potassium tungstate, and mixturesthereof, the nickel is provided from a nickel source selected from thegroup consisting of nickel chloride, nickel sulfate, nickel nitrate, andmixtures thereof, the cobalt is provided from a cobalt source selectedfrom the group consisting of cobalt chloride, cobalt fluoride, cobaltbromide, cobalt iodide, and mixtures thereof, the magnesium is providedfrom a magnesium source selected from the group consisting of magnesiumchloride, magnesium sulfate, magnesium phosphate, and the sulfur isprovided from a sulfur source selected from the group consisting ofcysteine, sodium sulfide, and mixtures thereof.
 15. The fermentationprocess of claim 8 wherein a pH of the fermentation medium is maintainedin a range of about 4.2 to about 4.8.
 16. The fermentation process ofclaim 8 wherein the syngas has a CO/CO₂ ratio of at least about 0.75.17. The fermentation process of claim 8 wherein the fermentationincludes contacting the syngas with one or more acetogenic bacteria. 18.The fermentation process of claim 17 wherein the acetogenic bacteria isselected from the group consisting of Acetogenium kivui, Acetoanaerobiumnoterae, Acetobacterium woodii, Alkalibaculum bacchi CP11 (ATCCBAA-1772), Blautia producta, Butyribacterium methylotrophicum,Caldanaerobacter subterraneous, Caldanaerobacter subterraneouspacificus, Carboxydothermus hydrogenoformans, Clostridium aceticum,Clostridium acetobutylicum, Clostridium acetobutylicum P262 (DSM 19630of DSMZ Germany), Clostridium autoethanogenum (DSM 19630 of DSMZGermany), Clostridium autoethanogenum (DSM 10061 of DSMZ Germany),Clostridium autoethanogenum (DSM 23693 of DSMZ Germany), Clostridiumautoethanogenum (DSM 24138 of DSMZ Germany), Clostridium carboxidivoransP7 (ATCC PTA-7827), Clostridium coskatii (ATCC PTA-10522), Clostridiumdrakei, Clostridium ljungdahlii PETC (ATCC 49587), Clostridiumljungdahlii ERI2 (ATCC 55380), Clostridium ljungdahlii C-01 (ATCC55988), Clostridium ljungdahlii O-52 (ATCC 55889), Clostridium magnum,Clostridium pasteurianum (DSM 525 of DSMZ Germany), Clostridium ragsdaliP11 (ATCC BAA-622), Clostridium scatologenes, Clostridiumthermoaceticum, Clostridium ultunense, Desulfotomaculum kuznetsovii,Eubacterium limosum, Geobacter sulfurreducens, Methanosarcinaacetivorans, Methanosarcina barkeri, Morrella thermoacetica, Morrellathermoautotrophica, Oxobacter pfennigii, Peptostreptococcus productus,Ruminococcus productus, Thermoanaerobacter kivui, and mixtures thereof.19. The fermentation process of claim 8 wherein the process is effectivefor providing a cell density of at least about 1.0 g/L
 20. Thefermentation process of claim 8 wherein the process is effective forproviding a CO conversion of at least about 5 to about 99%.